EP2186787A1 - Hydrogénation d'acide éthanoïque pour produire de l'éthanol - Google Patents

Hydrogénation d'acide éthanoïque pour produire de l'éthanol Download PDF

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EP2186787A1
EP2186787A1 EP08253723A EP08253723A EP2186787A1 EP 2186787 A1 EP2186787 A1 EP 2186787A1 EP 08253723 A EP08253723 A EP 08253723A EP 08253723 A EP08253723 A EP 08253723A EP 2186787 A1 EP2186787 A1 EP 2186787A1
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methanol
catalyst
process according
ethanoic acid
synthesis unit
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BP PLC
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Priority to EP08253723A priority Critical patent/EP2186787A1/fr
Priority to CN200980154495.0A priority patent/CN102282117B/zh
Priority to US12/998,639 priority patent/US8524954B2/en
Priority to PCT/GB2009/002639 priority patent/WO2010055285A1/fr
Priority to MYPI2011002090A priority patent/MY159190A/en
Priority to EP09749176A priority patent/EP2352714A1/fr
Publication of EP2186787A1 publication Critical patent/EP2186787A1/fr
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
    • C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
    • C07C51/12—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on an oxygen-containing group in organic compounds, e.g. alcohols
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

  • the present invention relates to the production of ethanol (and optionally methanol) from ethanoic acid.
  • the present invention relates to a process for the production of ethanol (and optionally methanol) from a carbonaceous feedstock; wherein.the ethanoic acid (produced by a multi-step process from the carbonaceous feedstock) is hydrogenated to produce ethanol within the same alcohol synthesis unit and in the presence of the same catalyst(s) that is used to produce the said methanol from the said synthesis gas.
  • the said alcohols may be produced by the fermentation of, for example, sugars and/or cellulosic materials.
  • Alcohols such as ethanol
  • Synthesis gas refers to a combination of H 2 and carbon oxides produced in a synthesis gas plant from a carbon source such as natural gas, petroleum liquids, biomass and other carbonaceous materials including coal, recycled plastics, municipal wastes, or any organic material.
  • a carbon source such as natural gas, petroleum liquids, biomass and other carbonaceous materials including coal, recycled plastics, municipal wastes, or any organic material.
  • alcohol and alcohol derivatives may provide non-petroleum based routes for the production of valuable chemicals and fuels.
  • synthesis gas preparation e.g. the feedstock is purified to remove sulphur and other potential catalyst poisons prior to being converted into synthesis gas.
  • This treatment can also be conducted after synthesis gas preparation; for example, when coal or biomass is employed.
  • the reaction to produce alcohol(s) from synthesis gas is generally exothermic.
  • the formation of C 2 and C 2+ alcohols is believed to proceed via the formation of methanol for modified methanol catalysts and cobalt molybdenum sulphide catalysts.
  • the production of methanol is equilibrium-limited and thus requires high pressures in order to achieve viable yields.
  • pressure can be used to increase the yield, as the reaction which produces methanol exhibits a decrease in volume, as disclosed in US 3326956 .
  • a low-pressure, copper-based methanol synthesis catalyst is commercially available from suppliers such as BASF, Johnson Matthey, and Haldor-Topsoe. Methanol yields from copper-based catalysts are generally over 99.5% of the converted CO+CO 2 present. Water is a by-product of the conversion of CO 2 to methanol and the conversion of CO synthesis gas to C 2 and C 2+ oxygenates. In the presence of an active water-gas shift catalyst, such as a methanol catalyst or a cobalt molybdenum catalyst the water equilibrates with the CO to give CO 2 and H 2 .
  • an active water-gas shift catalyst such as a methanol catalyst or a cobalt molybdenum catalyst the water equilibrates with the CO to give CO 2 and H 2 .
  • WO 8303409 describes a process whereby ethanol is produced by carbonylation of methanol by reaction with CO in the presence of a carbonylation catalyst to form ethanoic acid which is then converted to an ethanoate ester followed by hydrogenolysis of the ethanoate ester formed to give ethanol or a mixture of ethanol and another alcohol which can be separated by distillation.
  • Carbonylation can be effected using a CO/H 2 mixture and hydrogenolysis can similarly be conducted in the presence of CO, leading to the possibility of circulating gas between the carbonylation and hydrogenolysis zones with synthesis gas, preferably a 2:1 H 2 :CO molar mixture being used as make up gas.
  • US 4122110 relates to a process for manufacturing alcohols, particularly linear saturated primary alcohols, by reacting CO with H 2 at a pressure between 2 and 25 MPa and a temperature between 150 and 400 °C, in the presence of a catalyst, characterized in that the catalyst contains at least 4 essential elements: (a) copper (b) cobalt (c) at least one element M selected from chromium, iron, vanadium and manganese, and (d) at least one alkali metal.
  • US 4831060 relates to the production of mixed alcohols from CO and H 2 gases using a catalyst, with optionally a co-catalyst, wherein the catalyst metals are molybdenum, tungsten or rhenium, and the co-catalyst metals are cobalt, nickel or iron.
  • the catalyst is promoted with a Fischer-Tropsch promoter like an alkali or alkaline earth series metal or a smaller amount of thorium and is further treated by sulphiding.
  • the composition of the mixed alcohols fraction can be selected by selecting the extent of intimate contact among the catalytic components.
  • Journal of Catalysis, 1988, 114, 90-99 discloses a mechanism of ethanol formation from synthesis gas over CuO/ZnO/Al 2 O 3 .
  • the formation of ethanol from CO and H 2 over a CuO/ZnO methanol catalyst is studied in a fixed-bed microreactor by measuring the isotopic distribution of the carbon in the product ethanol when isotopically-enriched 13 C methanol was added to the feed.
  • the present invention provides a process that allows one to produce ethanol from a carbonaceous feedstock, with an improved carbon efficiency, a higher selectivity and, in particular, with a more productive conversion to ethanol.
  • Figure 1 represents an embodiment of a process scheme according to the present invention, wherein the references correspond to those used in the present description and appending claims.
  • the present invention relates to a process for producing methanol and ethanol, wherein the methanol is produced from synthesis gas and the ethanol is produced via the hydrogenation of an ethanoic acid feed; characterised in that the hydrogenation of the ethanoic acid feed is carried out with the same catalyst(s), and within the same alcohol synthesis unit, that is used to produce the said methanol from the said synthesis gas.
  • the present invention relates to a process for the conversion of synthesis gas to ethanol, characterised by the following steps:
  • the present invention relates to a process for the conversion of a carbonaceous feedstock(s) into ethanol, characterised by the following steps:
  • the synthesis gas feedstock, a mixture of carbon oxide(s) and H 2 , that is used to produce the methanol feed stream is preferably produced from a carbonaceous feedstock.
  • the carbonaceous feedstock is preferably a material such as biomass, plastic, naphtha, refinery bottoms, crude synthesis gas (from underground coal gasification or biomass gasification), smelter off gas, municipal waste, coal bed methane, coal, and/or natural gas, with coal and natural gas being the preferred sources.
  • a combination of sources can also be used, for example coal and natural gas to advantageously increase the H 2 to carbon ratio.
  • Natural gas commonly contains a range of hydrocarbons (e.g. C 1 -C 3 alkanes), in which methane predominates.
  • natural gas will usually contain nitrogen, CO 2 and sulphur compounds.
  • the nitrogen content of the feedstock is less than 40 mol %, more preferably less than 10 mol % and most preferably less than 2 mol %.
  • the synthesis gas may be obtained by catalytic partial oxidation of hydrocarbonaceous material in a microstructured reactor as exemplified in IMRET 3: Proceedings of the Third International Conference on Microreaction Technology, ed. W. Ehrfeld, Springer Verlag, 1999, pages 187-196 .
  • the synthesis gas may be obtained by short contact time catalytic partial oxidation of hydrocarbonaceous feedstocks as described in EP 0303438 .
  • the synthesis gas can also be obtained via a 'compact reformer' process as described in Hydrocarbon Engineering, 2000, 5:5, 67-69 ; Hydrocarbon Processing, 2000, 79:9, 34 ; Today's Refinery, 2000, 15:8, 9 ; WO 9902254 ; and WO 0023689 .
  • the pressure at which the synthesis gas is produced from a steam reformer ranges from approximately 0.1 to 10 MPa, preferably 2 to 3 MPa and the temperatures at which the synthesis gas exits the reformer ranges from approximately 700 to 1000°C.
  • the pressure at which the synthesis gas is produced from an auto-thermal reformer ranges from approximately 0.1 to 10 MPa, preferably 2 to 5 MPa and the temperatures at which the synthesis gas exits the reformer ranges from approximately 700 to 1300 °C. Where the high temperatures are necessary in order to produce a favourable equilibrium for synthesis gas production, and to avoid metallurgy problems associated with carbon dusting.
  • the synthesis gas contains a molar ratio of (H 2 -CO 2 ):(CO+CO 2 ) ranging from 0.8 to 3.0, which is dependent on the carbonaceous feedstock(s) and the method of reforming used. For example, when natural gas is used as the carbonaceous feedstock for steam reforming, the synthesis gas obtained usually has a maximum (H 2 -CO 2 ):(CO+CO 2 ) ratio of 3.0. However, when natural gas is used as the carbonaceous feedstock for auto-thermal reforming, the synthesis gas obtained usually has a (H 2 -CO 2 ):(CO+CO 2 ) ratio of 1.5.
  • the molar ratio, (H 2 -CO 2 ):(CO+CO 2 ), of the synthesis gas stream exiting the synthesis gas generation unit(s) is greater than 1.6, more preferably greater than 1.8 and most preferably greater than 2.0.
  • the molar ratio, (H 2 -CO 2 ):(CO+CO 2 ), of said synthesis gas stream exiting the synthesis gas generation unit(s) is less than 3.0, preferably less than 2.75, more preferably less than 2.4 and most preferably less than 2.2.
  • the carbonaceous feedstock used for synthesis gas generation is not an aliphatic hydrocarbon (e.g. coal, aromatic material, biomass)
  • the molar ratio (H 2 -CO 2 ):(CO+CO 2 ) of the exit synthesis gas is preferably adjusted to the target value by the addition of H 2 or the removal of CO 2 .
  • CO 2 may be removed by the use of a simple, yet effective, separation method known to those skilled in the art, for example, a "membrane separation method".
  • membrane technologies can be found in 'Purification and Recovery Options for Gasification' D. J. Kubek, E. Polla, F. P. Wilcher, UOP, 1996 .
  • CO 2 may be recovered and removed by any suitable method(s) known to those skilled in the art, for example, by reacting with amines; performing a methanol wash (i.e. the RECTISOL process) and/or by using hot potassium carbonate (e.g. the BENFIELD process).
  • a methanol wash i.e. the RECTISOL process
  • hot potassium carbonate e.g. the BENFIELD process
  • the exit stream obtained from the synthesis gas reactor comprises essentially a mixture of carbon oxide(s) and H 2 . It can also comprise water, nitrogen and traces of unconverted hydrocarbons (e.g. C 1 -C 3 alkanes).
  • an additional stage may be employed whereby the feedstock is first purified to remove sulphur and other potential catalyst poisons (such as halides or metals e.g. mercury) prior to being converted into synthesis gas; alternatively this treatment can also be performed after synthesis gas preparation for example, when coal or biomass are used.
  • sulphur and other potential catalyst poisons such as halides or metals e.g. mercury
  • synthesis gas is introduced into an alcohol synthesis unit, together with ethanoic acid to produce a stream comprising methanol and ethanol, in addition to unreacted ethanoic acid.
  • a synthesis gas stream is produced by the aforementioned synthesis gas generation process.
  • the stream exiting the alcohol synthesis unit is subsequently purified to remove said by-products by any methods known to those in the art to obtain substantially pure methanol and ethanol products.
  • the preferred molar ratio, (H 2 -CO 2 ):(CO+ CO 2 ) (where the concentrations of relevant components are expressed in volume percent or mole percent), of the fresh synthesis gas feed stream fed into the alcohol synthesis unit is greater than 3.0, more preferably greater than 4.0 and most preferably greater than 4.1.
  • the molar ratio, (H 2 -CO 2 ):( CO+ CO 2 ) of the fresh synthesis gas feed stream fed into the alcohol synthesis unit is less than 8.5, preferably less than 5.0 and most preferably less than 4.4.
  • CO 2 represents more than 1 vol%, preferably more than 2 vol% and most preferably more than 5 vol% of the total alcohol synthesis reactor gas phase composition.
  • H 2 In order to obtain the aforementioned high synthesis gas molar ratios, additional H 2 needs to be added to the synthesis gas feed stream exiting the synthesis gas generation unit.
  • this said H 2 is obtained from the aforementioned synthesis gas generation stage. This is preferably performed by first removing CO 2 and water from the generated synthesis gas followed by a cryogenic separation to isolate the substantially pure CO from the H 2 .
  • Alternative methods of separation, such as membrane separation technologies can also be employed.
  • said H 2 stream may also be obtained from another suitable source, such as another chemical process (e.g. off-gas from steel manufacture or electrolysis).
  • Said H 2 stream(s) may still contain inert impurities such as methane, nitrogen, noble gases, water and C 1 to C 4 paraffinic hydrocarbons, which are preferably removed before use.
  • An added advantage of this aspect of the present invention when compared to other processes in the field, is that the purification of the separated H 2 feed produced during synthesis gas generation has no requirement for the removal of carbon oxides. Indeed, this is advantageous when compared to a process with a separate hydrogenation stage for ethanoic acid where the carbon oxides act as poisons to the hydrogenation catalyst as well as increasing the formation of inert materials, thus necessitating an increased purge step.
  • the alcohol synthesis unit may be any reactor that is suitable for producing methanol and ethanol, for example a fluidised bed reactor or a fixed bed reactor, which can be run with or without external heat exchange equipments e.g. a multi-tubular reactor; or a fluidised bed reactor; or a void reactor.
  • a fluidised bed reactor or a fixed bed reactor which can be run with or without external heat exchange equipments e.g. a multi-tubular reactor; or a fluidised bed reactor; or a void reactor.
  • the alcohol synthesis unit is operated at a temperature of more than 180 °C, preferably more than 200 °C and most preferably more than 220 °C; and less than 290 °C, preferably less than 280 °C, more preferably less than 270 °C and most preferably less than 250 °C.
  • the alcohol synthesis unit is operated at pressure of more than 2 MPa and preferably more than 5 MPa; and less than 10 MPa and preferably less than 9MPa.
  • the chosen temperature of operation is governed by a balance of promoting the forward reaction (i.e. by not adversely affecting the equilibrium) and aiding the rate of conversion (i.e. higher productivity).
  • the ethanol synthesis is also exothermic; however, in this case the chosen temperature of operation is governed by a balance of reaction rate and selectivity.
  • the GHSV for continuous operation may be in the range 50 to 50,000 h -1 , preferably from 1,000 to 30,000 h -1 , more preferably from 2,000 to 18,000 h -1 and most preferably from 5,000 to 12,000 h -1 .
  • the ethanoic acid liquid substrate introduced into the alcohol synthesis unit preferably has an LHSV less than 10 h -1 , more preferably less than 5 h -1 and most preferably less than 3 h -1 ; for example, a typical LHSV for normal operation is approximately 1 h -1 .
  • a key feature of the present invention is that the synthesis of methanol from synthesis gas and the hydrogenation of ethanoic acid to ethanol occurs in the same alcohol synthesis unit. Therefore the catalyst for methanol synthesis from synthesis gas and the catalyst for ethanoic acid hydrogenation may be one and the same catalyst; or alternatively more than one catalyst may be employed in the alcohol synthesis unit.
  • the catalyst, or catalysts may be any suitable catalyst known to those skilled in the art to catalyse the synthesis of methanol from synthesis gas and those which are known to those skilled in the art to catalyse the hydrogenation of carboxylic acids and/or esters to alcohols.
  • the hydrogenation catalyst is located downstream of said methanol synthesis catalyst; thus, according to a preferred embodiment of the present invention, the catalyst configuration of the alcohol synthesis unit is such that the stream(s) comprising CO, H 2 and ethanoic acid, is first reacted in the presence of a methanol synthesis catalyst and subsequently reacted in the presence of a hydrogenation catalyst.
  • the catalyst for the alcohol synthesis unit can be chosen amongst traditional methanol synthesis catalysts selected from one of the two following groups:
  • a preferred methanol synthesis catalyst is a mixture of copper, zinc oxide, and a promoter such as chromia or alumina. The Applicants have unexpectedly found that the said methanol synthesis catalyst demonstrated high hydrogenation activities.
  • the preferred catalyst used in the alcohol synthesis unit is either a hydrogenation catalyst or consists of a mixture of the above methanol catalyst together with a hydrogenation catalyst.
  • the hydrogenation catalyst can be selected from the following:
  • the hydrogenation catalyst (which may be mixed with the methanol catalyst) is a copper based catalyst, most preferably comprising copper and zinc.
  • All of the aforementioned hydrogenation catalysts may advantageously be supported on any suitable support known to those skilled in the art; non-limiting examples of such supports include carbon, silica, titania, clays, aluminas, zinc oxide, zirconia and mixed oxides.
  • the palladium based catalyst is supported on carbon.
  • the copper based catalyst is supported on zinc oxide.
  • At least a part of the stream exiting the alcohol synthesis unit is passed through a separation unit (e.g. a separation column) to recover and collect a stream comprising the targeted ethanol and a stream comprising methanol.
  • a separation unit e.g. a separation column
  • This separation stage may be performed by any suitable means known to those skilled in the art, e.g. a sieve tray column, a packed column, a bubble cap column or a combination thereof.
  • the streams exiting the separation zone are subsequently purified to remove said by-products from the methanol and ethanol streams by any methods known to those skilled in the art.
  • At least a part of the aforementioned stream comprising methanol (and optionally methyl ethanoate), together with a substantially pure CO stream are introduced into a carbonylation reactor.
  • said methanol stream may also emanate from another suitable source, such as a bio-fermentation process and/or pyrolysis (e.g. wood pyrolysis).
  • At least a part of the said CO stream is obtained from the aforementioned synthesis gas generation stage. This is preferably performed by first removing CO 2 and water from the generated synthesis gas followed by a cryogenic separation to isolate the substantially pure CO from the H 2 .
  • a particular advantage according to the present invention is that both the H 2 fed to the alcohol synthesis unit and the CO fed to the carbonylation unit are obtained from the same synthesis gas separation stage. Alternative methods of separation, such as membrane separation technologies can also be employed.
  • said CO stream may also be obtained from another suitable source, such as another chemical process (e.g. off-gas from steel manufacture).
  • Said substantially pure CO stream may contain inert impurities such as CO 2 , methane, nitrogen, noble gases, water and C 1 to C 4 paraffinic hydrocarbons which are preferably removed before use.
  • the step of introducing methanol, together with CO, into a carbonylation reactor is performed under conditions favourable for producing ethanoic acid.
  • Such carbonylation processes can be made in the presence of iridium catalysts as described in US 3772380 .
  • UK patent GB 1276326 also describes the preparation of mono-carboxylic acids by carbonylation of alcohols in the presence of rhodium or iridium catalysts, halogen promoters and water or an alcohol, ether or ester.
  • UK patent application GB 2029409 describes a process for the preparation of aliphatic carboxylic acids by reacting CO with alcohols at an elevated pressure of 3.4 MPa or greater in the presence of a ruthenium catalyst and halogen-containing promoter.
  • the carbonylation process takes place in the presence of an iridium catalyst together with at least one promoter; indeed, such catalyst systems have proven to have beneficial effects on the rate of carbonylation of methanol.
  • Said carbonylation process is thus preferably performed in the presence of at least a finite concentration of water with a catalyst system comprising:
  • the process for the production of ethanoic acid by carbonylation of methanol comprises contacting methanol with CO, in the liquid reaction composition, in a carbonylation reactor wherein, the liquid reaction composition comprises:
  • water may be formed in situ in the liquid reaction composition.
  • water may be produced via by-product formation, generated during methane production.
  • Water may also be generated during the esterification reaction between methanol reactant and ethanoic acid product.
  • Water may also be introduced to the carbonylation reactor together with, or separately from, other components of the liquid reaction composition.
  • Water may be separated from other components of reaction composition withdrawn from the reactor and may be recycled in controlled amounts to maintain a preferred concentration of water in the liquid reaction composition.
  • the concentration of water in the liquid reaction composition of the carbonylation reactor is in the range 0.1 to 15 wt %, more preferably 1 to 10 wt %, most preferably 1 to 6.5 wt %.
  • the iridium catalyst in the liquid reaction composition may comprise any iridium containing compound which is soluble in the liquid reaction composition.
  • the iridium catalyst may be added to the liquid reaction composition for the carbonylation reaction in any suitable form which dissolves in the liquid reaction composition or is convertible to a soluble form.
  • the iridium carbonylation catalyst concentration in the liquid reaction composition is in the range 100 to 6000 ppm by weight of iridium, more preferably 700 to 3000 ppm by weight of iridium.
  • At least one promoter is present in the reaction composition.
  • Suitable promoters are preferably selected from the group consisting of ruthenium, osmium, rhenium, cadmium, mercury, zinc, gallium, indium and tungsten, and are more preferably selected from ruthenium and osmium and most preferably is ruthenium.
  • the promoter is present in an effective amount up to the limit of its solubility in the liquid reaction composition and/or any liquid process streams recycled to the carbonylation reactor from the ethanoic acid recovery stage.
  • the promoter is suitably present in the liquid reaction composition at a molar ratio of promoter : iridium of [0.5 to 15] : 1.
  • promoter such as ruthenium
  • a suitable promoter concentration is 400 to 5000 ppm by weight.
  • the promoter may comprise any suitable promoter metal-containing compound which is soluble in the liquid reaction composition.
  • the promoter may be added to the liquid reaction composition for the carbonylation reaction in any suitable form which dissolves in the liquid reaction composition or is convertible to soluble form.
  • osmium (III) chloride hydrate and anhydrous osmium metal, osmium tetraoxide, triosmiumdodecacarbonyl, [O s (CO) 4 I 2 ], [Os(CO) 3 I 2 ] 2 , [Os(CO) 3
  • Suitable rhenium-containing compounds which may be used as sources of promoter include Re 2 (CO) 10 , Re(CO) 5 Cl, Re(CO) 5 Br, Re(CO) 5 I, ReCl 3 .xH 2 O, [Re(CO) 4 I] 2 , [Re(CO) 4 I 2 ] - H + , and ReCl 5 .yH 2 O.
  • Suitable cadmium-containing compounds include Cd(OAc) 2 , CdI 2 , CdBr 2 , CdCl 2 , Cd(OH) 2 , and cadmium acetylacetonate.
  • suitable mercury-containing compounds which may be used as sources of promoter include Hg(OAc) 2 , HgI 2 , HgBr 2 , HgCl 2 , Hg 2 I 2 , and Hg 2 Cl 2 .
  • suitable zinc-containing compounds which may be used as sources of promoter include Zn(OAc) 2 , Zn(OH) 2 , ZnI 2 , ZnBr 2 , ZnCl 2 , and zinc acetylacetonate.
  • suitable gallium-containing compounds which may be used as sources of promoter include gallium acetylacetonate, gallium ethanoate, GaCl 3 , GaBr 3 , GaI 3 , Ga 2 Cl 4 and Ga(OH) 3 .
  • the iridium- and promoter-containing compounds are free of impurities which provide or generate in situ ionic iodides which may inhibit the reaction, for example, alkali or alkaline earth metal or other metal salts.
  • Ionic contaminants such as, for example, (a) corrosion metals, particularly nickel, iron and chromium and (b) phosphines or nitrogen containing compounds or ligands which may quaternise in situ; should be kept to a minimum in the liquid reaction composition as these will have an adverse effect on the reaction by generating I - in the liquid reaction composition which has an adverse effect on the reaction rate.
  • Some corrosion metal contaminants such as for example molybdenum have been found to be less susceptible to the generation of I - .
  • Corrosion metals which have an adverse affect on the reaction rate may be minimised by using suitable corrosion-resistant materials of construction.
  • contaminants such as alkali metal iodides, for example lithium iodide, should be kept to a minimum.
  • Corrosion metal and other ionic impurities may be reduced by the use of a suitable ion exchange resin bed to treat the reaction composition, or preferably a catalyst recycle stream. Such a process is described in US 4007130 .
  • ionic contaminants are kept below a concentration at which they would generate 500 ppm by weight of I - , preferably less than 250 ppm by weight of I - in the liquid reaction composition.
  • the concentration of methyl iodide in the liquid reaction composition is in the range 1 to 20 wt %, preferably 5 to 16 wt %.
  • the partial pressure of CO in the carbonylation reactor is suitably in the range 0.1 to 7 MPa preferably 0.1 to 3:5 MPa and most preferably 0.1 to 1.5 MPa.
  • the presence of H 2 in the CO feed and generated in situ by the water-gas shift reaction is preferably kept low as its presence may result in the formation of hydrogenation products.
  • the molar ratio of H 2 to CO reactant is preferably less than 0.01:1, more preferably less than 0.005:1 and yet more preferably less than 0.003:1 and/or the partial pressure of H 2 in the carbonylation reactor is preferably less than 0.1 MPa, more preferably less than 0.05 MPa and yet more preferably less than 0.03 MPa.
  • the catalyst system used in the carbonylation process of this aspect of the present invention has been found to be particularly beneficial at relatively low partial pressures of CO where the rate of reaction may be dependent upon the CO partial pressure. Under these conditions, it has been found that the catalyst system has the advantage of providing an increased rate of reaction over catalyst systems without the promoters of the present invention. This advantage allows for an increased rate of reaction under conditions when the CO partial pressure is relatively low, for example due to a low total pressure in the carbonylation reactor or due to high vapour pressure of components of the liquid reaction composition, e.g. at high methyl ethanoate concentration in the liquid reaction composition or due to a high concentration of inert gases (for example nitrogen and CO 2 in the carbonylation reactor.
  • the catalyst system may also have advantages of increasing rate of carbonylation when the rate of reaction is reduced by the availability of CO in solution in the liquid reaction composition resulting from mass transfer limitations, for example due to poor agitation.
  • the pressure of the carbonylation reaction is suitably in the range 0.9 to 19.9 MPa, preferably 0.9 to 9.9 MPa, most preferably 1.4 to 4.9 MPa.
  • the temperature of the carbonylation reaction is suitably in the range 100 to 300 °C, preferably in the range 150 to 220 °C.
  • Ethanoic acid may advantageously be used as a solvent for said carbonylation reaction.
  • the carbonylation process of the present invention may be performed as a batch or continuous process, preferably as a continuous process and may be performed in any suitable reactor, known to those skilled in the art.
  • the ethanoic acid product may be removed from the reactor by withdrawing liquid reaction composition and separating the ethanoic acid product by one or more flash and/or fractional distillation stages from the other components of the liquid reaction composition such as iridium catalyst, ruthenium and/or osmium and/or indium promoter, methyl iodide, water and unconsumed reactants which may be recycled to the reactor to maintain their concentrations in the liquid reaction composition.
  • the ethanoic acid product may also be removed as a vapour from the stream exiting the carbonylation reactor.
  • halide promoters and stabilizers such as methyl iodide
  • the continued presence of halide compounds in the carbonylation reaction products is undesirable if the product is employed as a starting material in a subsequent process employing a halide-sensitive catalyst where poisoning effects may be cumulative and irreversible.
  • the ethanoic acid product is purified of halide compounds. This purification treatment can be achieved by any appropriate method known to those skilled in the art.
  • halides can be removed from the liquid phase using silver salts either unsupported, or supported, on an ion-exchange resin or a zeolite as exemplified in US 5344976 and references therein.
  • the separated ethanoic acid from the stream exiting the carbonylation reactor is purified to remove carbonylation catalyst and water, before its introduction into the alcohol synthesis unit.
  • the ethanoic acid stream contains preferably less than 0.1 ppm wt of carbonylation catalyst, more preferably less than 0.05 ppm wt, most preferably less than 0.005 ppm wt.
  • At least a part, preferably all, of the said ethanoic acid feed stream originates from the aforementioned carbonylation reaction; however in practice, it may also originate from another suitable source, such as wood pyrolysis and/or as a by-product of a fermentation process to produce alcohol(s).
  • the ethanoic acid stream contains preferably less than 20 mol % of water.
  • water represents between 0.5 and 20 mol %, preferably between 0.5 and 15 mol % and most preferably between 1 and 5 mol % of the total liquid feed (ethanoic acid and water) to the alcohol synthesis unit.
  • the ethanoic acid fed into the alcohol synthesis unit is preferably purified of sulphur and halide compounds.
  • This purification treatment can be achieved by any appropriate method known to those skilled in the art.
  • halides and iodides can be removed in the liquid phase using silver salts (either homogeneous or supported) on either an ion-exchange resin or a zeolite, or for the removal of sulphides the purification treatment may be performed in the vapour phase, by passing the vapour over a sacrificial bed of zinc oxide (or copper zinc oxides).
  • the ethanoic acid feed is preferably vapourised prior to contacting the alcohol synthesis catalyst by either, heating the ethanoic acid in a separate vapouriser prior to having contact with the synthesis gas or, by heating the ethanoic acid within the synthesis gas (e.g. either in a separate vessel or on a prebed to the alcohol synthesis reactor).
  • the feed mixture including recycles entering the alcohol synthesis unit e.g. the synthesis gas, together with the ethanoic acid

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  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP08253723A 2008-11-13 2008-11-13 Hydrogénation d'acide éthanoïque pour produire de l'éthanol Ceased EP2186787A1 (fr)

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Application Number Priority Date Filing Date Title
EP08253723A EP2186787A1 (fr) 2008-11-13 2008-11-13 Hydrogénation d'acide éthanoïque pour produire de l'éthanol
CN200980154495.0A CN102282117B (zh) 2008-11-13 2009-11-10 乙酸氢化制造乙醇
US12/998,639 US8524954B2 (en) 2008-11-13 2009-11-10 Hydrogenation of ethanoic acid to produce ethanol
PCT/GB2009/002639 WO2010055285A1 (fr) 2008-11-13 2009-11-10 Hydrogénation d’acide éthanoïque pour produire de l’éthanol
MYPI2011002090A MY159190A (en) 2008-11-13 2009-11-10 Hydrogenation of ethanoic acid to produce ethanol
EP09749176A EP2352714A1 (fr) 2008-11-13 2009-11-10 Hydrogénation d acide éthanoïque pour produire de l éthanol

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EP09749176A Withdrawn EP2352714A1 (fr) 2008-11-13 2009-11-10 Hydrogénation d acide éthanoïque pour produire de l éthanol

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CN (1) CN102282117B (fr)
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